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EP0225817B1 - Procédé et installation de traitement à l'ammoniac - Google Patents

Procédé et installation de traitement à l'ammoniac Download PDF

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Publication number
EP0225817B1
EP0225817B1 EP86402322A EP86402322A EP0225817B1 EP 0225817 B1 EP0225817 B1 EP 0225817B1 EP 86402322 A EP86402322 A EP 86402322A EP 86402322 A EP86402322 A EP 86402322A EP 0225817 B1 EP0225817 B1 EP 0225817B1
Authority
EP
European Patent Office
Prior art keywords
ammonia
liquid
gas
washing
treatment
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired
Application number
EP86402322A
Other languages
German (de)
English (en)
French (fr)
Other versions
EP0225817A1 (fr
Inventor
Jean-Renaud Brugerolle
Michel Combe
Joseph Paganessi
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Priority to AT86402322T priority Critical patent/ATE45761T1/de
Publication of EP0225817A1 publication Critical patent/EP0225817A1/fr
Application granted granted Critical
Publication of EP0225817B1 publication Critical patent/EP0225817B1/fr
Expired legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
    • C10K1/10—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids
    • C10K1/12—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids alkaline-reacting including the revival of the used wash liquors
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B32/00—Carbon; Compounds thereof
    • C01B32/50—Carbon dioxide

Definitions

  • the present invention relates to the technique of treating ammonia gases. It applies in particular to the recovery of C0 2 from fumes relatively poor in C0 2 such as combustion fumes, which contain 8 to 20% thereof, or fumes from cement factories or lime kilns, which contain it 20 to 50%. It can thus be applied to other types of gas treatment available at high temperature, for example the purification of acid gases, in particular of fumes containing impurities SO x , NO x or HCL, before their rejection in the atmosphere or their subsequent treatment with PSA (Pressure Swing Adsorption).
  • PSA Pressure Swing Adsorption
  • ammonia is an absorption agent which is interesting in terms of its properties and its moderate cost, but which poses a difficult problem with regard to the gaseous release of installation. Indeed, this discharge contains a relatively large content of ammonia, and it is necessary to recover it both for economic reasons and to avoid pollution of the environment.
  • the object of the invention is to provide a method and an installation making it possible to solve this problem in a particularly economical manner.
  • the subject of the invention is a process for the treatment with ammonia of a gas available at high temperature, characterized in that the ammonia is removed from a gaseous effluent from the treatment by washing by means of a liquid essentially consisting of water, the washing liquid is regenerated by distillation against the current of the gas to be treated, then at least most of the regenerated washing liquid is recycled by putting it in heat exchange relationship with the washing liquid to be regenerated.
  • ammonia treatment has at least one slow kinetic reaction, as is the case for the absorption of C0 2 , according to a first embodiment of the invention, downstream of said distillation, circulates the gas to be treated in an absorption device supplied with an ammoniacal solution, then the ammonia is removed from the gaseous effluent of this device by said washing.
  • the liquid effluent leaving the absorption apparatus is desorbed by reducing the pressure.
  • the reaction targeted is sufficiently rapid, as is the case for the purification of acid fumes, according to another embodiment of the invention, downstream of said distillation; the gas is subjected directly to said washing, so that said ammonia treatment consists of said regeneration of the washing liquid.
  • the smoke can then be subjected, if necessary, to a treatment which exhibits at least one slow kinetic reaction, such as decarbonation.
  • the invention also relates to an installation intended for the implementation of the above method.
  • This installation includes a washing tower fed at its base by the gaseous effluent from the ammonia treatment apparatus and at its top by a liquid essentially consisting of water, a distillation apparatus whose top is connected by a first pipe at the base of the washing tower and which is supplied at its base with the gas to be treated, and a recycling pipe, in heat exchange relationship with said first pipe, which connects the base of the device distillation at the top of the wash tower.
  • the installation illustrated in FIG. 1 essentially comprises an absorption column 1, a vacuum desorption device 2 and a unit for washing with water 3.
  • the liquid streams are indicated in thin lines. thick lines the gas streams.
  • the absorption column 1 is supplied at its base with smoke from a source 4 via a pipe 5 provided with a blower or fan 6. In column 1, this smoke rises against stream of an ammoniacal solution which absorbs C0 2 , this at a temperature close to ambient temperature (for example of the order of 10 to 30 ° C) and at a pressure close to atmospheric pressure.
  • the ammoniacal solution is brought to a dispensing device 7 placed at the head of the column 1 by a pipe 8 equipped with a flow control valve 9.
  • the device 2 for desorption or regeneration under vacuum essentially comprises two expansion pots 10, 11.
  • the first pot 10 is connected to the tank of the column 1 by a line 12 provided with an expansion valve 13; from the top of this pot leaves a production line 14 equipped with a vacuum pump 15 and, downstream thereof, a phase separator 16.
  • the bottom of the pot 10 is connected to the pot 11 by another pipe 17 provided with an expansion valve 18, while the top of the pot 11 is connected to the pot 10 by a pipe 19 fitted with a vacuum pump 20.
  • a first level of depression for example a pressure ab solution of 200 mm Hg (approximately 26,000 Pa), which constitutes the suction pressure of the pump 15, which discharges towards the separator 16 at approximately atmospheric pressure
  • a second level can be maintained in the pot 11 lower vacuum, for example an absolute pressure of 100 mm Hg (about 13,000 Pa), the pump 20 aspirating at this pressure and delivering at 200 mm Hg (about 26,000 Pa).
  • a recirculation pump 21 includes a suction orifice connected to the bottom of the pot 11 by a pipe 22, and a discharge orifice connected to the pipe 8.
  • a withdrawal branch 23 provided with a valve 24 is tapped on pipe 22, and a device 25 for supplying ammonia solution in addition to the desired content is inserted into line 8.
  • the washing unit 3 comprises a washing column 26 interposed in a pipe 27 for discharging the gaseous effluent produced at the top of the column 1, and a column 28 for regenerating the washing water interposed in the pipe 5 of smoke to be treated.
  • the bottom of the column 26 is connected to the top of the column 28 by a pipe 29, while the bottom of the column 28 is connected to the suction of a recycling pump 30 by a pipe 31, the discharge of this pump being connected to the top of the column 26 by a pipe 32.
  • the pipes 29 and 32 are put into heat exchange relationship by a heat exchanger 33, and the pipe 32 is equipped, downstream of the latter, with a cooler complementary 34 to water or air.
  • a draw-off branch 35 provided with a valve 36 is tapped on line 31, and a line 37 for supplying additional water is tapped on line 32.
  • the liquid remaining in the pot 11 is recycled by the pump 21 to the column 1 via the lines 22 and 8.
  • the flash gas produced in the pot 11 is returned by the pump 20, via the line 19, to the pot 10, where part of the water and the ammonia it contained is condensed.
  • the remaining gas and the flash gas produced in the pot 10 are evacuated together by the pump 15, via the pipe 14; the compression provided by this pump makes it possible to separate the water and the ammonia in liquid form therefrom in the separator 16, and it is gas containing more than 99% of C0 2 , constituting the product of the installation, which leaves this separator to be further processed in a conventional manner.
  • a small part of the liquid flow passing through line 22 can be eliminated if necessary through line 23 to avoid the concentration of the solution in reaction products of ammonia with the impurities SO x , NOx when these are present in the initial smoke.
  • an identical complement flow is supplied by the device 25.
  • the smoke contains for example 0.5 to 3% of ammonia, due to the partial pressure of the ammonia above the solution. It is therefore necessary to purify this effluent and, for this, the overhead gas from column 1 is sent through line 27 to washing column 26, where practically all the ammonia is absorbed by the water arriving in column head via line 32, with a flow rate of the order of 5 to 10% of that of the ammoniacal solution which feeds column 1.
  • the decarbonated gas which leaves column 26 and is evacuated to the atmosphere at 27A respects thus the admissible standards for the ammonia content.
  • column 28 is used both to cool the smoke from source 4, which is favorable for absorption in column 1, and for regenerating the washing water of the gaseous effluent from the installation, which makes it possible to recover the ammonia absorbed by the water and at the same time avoid environmental pollution.
  • the regenerated hot water collected in the bottom of the column 28 is recycled by the pump 30 via the pipes 31 and 32, precooled in the exchanger 33 and cooled to around ambient temperature in the exchanger 34.
  • a small part water flow can again be removed, if necessary, via line 35, to avoid the concentration of SOx, NOx impurities, the additional water being supplied through line 37.
  • the low flow of washing water required compared to the flow of the ammonia solution is advantageous in several aspects: on the one hand, the power of the pump 30 is low; on the other hand, the heat supplied by the smoke is sufficient to effectively regenerate the washing water and, consequently, to obtain a very low release of ammonia to the atmosphere via the 27 A pipe.
  • FIG. 2 represents the diagram of a similar installation corresponding to the case where the treatment with ammonia comprises only reactions with rapid kinetics.
  • This treatment takes place in the column 28 itself, which is therefore confused with the apparatus 1, while the desorption takes place in the tower 26, which is therefore confused with the desorption device 2A.
  • line 5 directly connects the top of column 28 to the base of tower 26 and is therefore merged with line 27 which carries the gaseous effluent from the ammonia treatment.
  • ammonia solution is made at 38 in line 29, downstream of the heat exchanger 33, to control the treatment in column 28.
  • an ammonia flow rate adjusted by an analyzer of the ammonia content of the water circulating in the pipe 29.
  • the drawing off 35A takes place, in the example shown, in the upper part of the column 28.
  • the smoke to be treated originating at high temperature from the source 4, is slightly compressed by the fan 6 and sent to the base of the distillation column 28 through the pipe 5.
  • the smoke makes it possible to regenerate, thanks to the heat that it contains water loaded with ammonia which arrives at the head of column 28 via line 29, coming from the washing tower.
  • the regenerated solution leaves the bottom of column 28 via line 31 and is recycled by pump 30 to column 26 through line 32, via heat exchangers 33 and 34.
  • the temperature prevailing in column 28 is slightly higher at room temperature, for example of the order of 30 to 50 ° C.
  • the impurities of the smoke react with the ammoniacal solution diluted in the upper part of column 28.
  • a small part of the liquid flow is withdrawn from column 28 by line 35, 35A or 35B , in order to remove the impurities from the smoke thus absorbed.
  • the smoke then contains for example 0.5 to 3% of ammonia, which will be absorbed in tower 26 by the cold regenerated solution, consisting of almost pure water, which arrives at the top of this tower and is brought into contact with the smoke against the current, this at a temperature close to ambient (for example 10 at 40 ° C).
  • the ammonia-purified smoke leaves the top of the tower 26 via line 27A, with a view to its rejection to the atmosphere or its further treatment.
  • the smoke can, for example, then be decarbonated by a P.S.A. system, the presence of SOx, NOx and NHs in the smoke of which would have seriously reduced the performance.
  • the ammonia-laden washing solution leaves column 26 via line 29 and, after being heated in the exchanger 33, feeds the top of column 28, which it crosses from top to bottom against the flow of smoke. treat.
  • the invention applies to the treatment with ammonia of various gaseous mixtures available at high temperature, whether at a pressure close to atmospheric pressure or at a higher pressure.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Inorganic Chemistry (AREA)
  • Analytical Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Treating Waste Gases (AREA)
  • Gas Separation By Absorption (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Industrial Gases (AREA)
EP86402322A 1985-10-25 1986-10-16 Procédé et installation de traitement à l'ammoniac Expired EP0225817B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT86402322T ATE45761T1 (de) 1985-10-25 1986-10-16 Verfahren und vorrichtung zur behandlung mit ammoniak.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR8515864A FR2589142B1 (fr) 1985-10-25 1985-10-25 Procede et installation de production d'anhydride carbonique a partir d'un gaz disponible a une pression voisine de la pression atmospherique
FR8515864 1985-10-25

Publications (2)

Publication Number Publication Date
EP0225817A1 EP0225817A1 (fr) 1987-06-16
EP0225817B1 true EP0225817B1 (fr) 1989-08-23

Family

ID=9324196

Family Applications (1)

Application Number Title Priority Date Filing Date
EP86402322A Expired EP0225817B1 (fr) 1985-10-25 1986-10-16 Procédé et installation de traitement à l'ammoniac

Country Status (21)

Country Link
US (1) US4847057A (ja)
EP (1) EP0225817B1 (ja)
JP (1) JPH0757304B2 (ja)
KR (1) KR880700049A (ja)
AR (1) AR240989A1 (ja)
AT (1) ATE45761T1 (ja)
AU (1) AU584476B2 (ja)
BR (1) BR8606945A (ja)
CA (1) CA1288580C (ja)
DE (1) DE3665193D1 (ja)
DK (1) DK320687A (ja)
ES (1) ES2010504B3 (ja)
FR (1) FR2589142B1 (ja)
GR (1) GR3000186T3 (ja)
MA (1) MA20799A1 (ja)
NZ (1) NZ218037A (ja)
OA (1) OA08621A (ja)
PT (1) PT83611B (ja)
TN (1) TNSN86146A1 (ja)
WO (1) WO1987002696A1 (ja)
ZA (1) ZA868115B (ja)

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US8182577B2 (en) * 2007-10-22 2012-05-22 Alstom Technology Ltd Multi-stage CO2 removal system and method for processing a flue gas stream
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US7846240B2 (en) * 2008-10-02 2010-12-07 Alstom Technology Ltd Chilled ammonia based CO2 capture system with water wash system
US8404027B2 (en) * 2008-11-04 2013-03-26 Alstom Technology Ltd Reabsorber for ammonia stripper offgas
US8292989B2 (en) * 2009-10-30 2012-10-23 Alstom Technology Ltd Gas stream processing
EP2427260A1 (en) * 2009-05-08 2012-03-14 Alstom Technology Ltd Heat recovery from a carbon dioxide capture and compression process for fuel treatment
US8784761B2 (en) * 2009-11-20 2014-07-22 Alstom Technology Ltd Single absorber vessel to capture CO2
US8309047B2 (en) 2009-09-15 2012-11-13 Alstom Technology Ltd Method and system for removal of carbon dioxide from a process gas
US8790605B2 (en) * 2009-09-15 2014-07-29 Alstom Technology Ltd Method for removal of carbon dioxide from a process gas
US8518156B2 (en) * 2009-09-21 2013-08-27 Alstom Technology Ltd Method and system for regenerating a solution used in a wash vessel
EP2322265A1 (en) * 2009-11-12 2011-05-18 Alstom Technology Ltd Flue gas treatment system
US20110146489A1 (en) * 2009-12-17 2011-06-23 Alstom Technology Ltd Ammonia removal, following removal of co2, from a gas stream
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US8728209B2 (en) 2010-09-13 2014-05-20 Alstom Technology Ltd Method and system for reducing energy requirements of a CO2 capture system
US8623307B2 (en) 2010-09-14 2014-01-07 Alstom Technology Ltd. Process gas treatment system
US8329128B2 (en) 2011-02-01 2012-12-11 Alstom Technology Ltd Gas treatment process and system
US9028784B2 (en) 2011-02-15 2015-05-12 Alstom Technology Ltd Process and system for cleaning a gas stream
US9427695B2 (en) * 2011-04-06 2016-08-30 Alstom Technology Ltd Carbon dioxide capture system
US9162177B2 (en) 2012-01-25 2015-10-20 Alstom Technology Ltd Ammonia capturing by CO2 product liquid in water wash liquid
US8864879B2 (en) 2012-03-30 2014-10-21 Jalal Askander System for recovery of ammonia from lean solution in a chilled ammonia process utilizing residual flue gas
US9740214B2 (en) 2012-07-23 2017-08-22 General Electric Technology Gmbh Nonlinear model predictive control for chemical looping process
US20140196499A1 (en) * 2013-01-14 2014-07-17 Alstom Technology Ltd. Stripper overhead heat integration system for reduction of energy consumption
US9447996B2 (en) 2013-01-15 2016-09-20 General Electric Technology Gmbh Carbon dioxide removal system using absorption refrigeration
US20140205524A1 (en) * 2013-01-24 2014-07-24 David Sevier Gas Component Extraction from Gas Mixture
US8986640B1 (en) 2014-01-07 2015-03-24 Alstom Technology Ltd System and method for recovering ammonia from a chilled ammonia process
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Also Published As

Publication number Publication date
FR2589142B1 (fr) 1988-01-08
JPH0757304B2 (ja) 1995-06-21
ZA868115B (en) 1987-06-24
AU584476B2 (en) 1989-05-25
CA1288580C (fr) 1991-09-10
TNSN86146A1 (fr) 1990-01-01
BR8606945A (pt) 1987-11-03
KR880700049A (ko) 1988-02-15
MA20799A1 (fr) 1987-07-01
DE3665193D1 (en) 1989-09-28
PT83611A (fr) 1986-11-01
ATE45761T1 (de) 1989-09-15
US4847057A (en) 1989-07-11
JPS63501549A (ja) 1988-06-16
NZ218037A (en) 1989-03-29
AR240989A1 (es) 1991-04-30
PT83611B (pt) 1988-10-14
DK320687D0 (da) 1987-06-24
ES2010504B3 (es) 1989-11-16
OA08621A (fr) 1988-11-30
DK320687A (da) 1987-06-24
AR240989A2 (es) 1991-04-30
GR3000186T3 (en) 1990-12-31
FR2589142A1 (fr) 1987-04-30
EP0225817A1 (fr) 1987-06-16
AU6529486A (en) 1987-05-19
WO1987002696A1 (fr) 1987-05-07

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